WO2004046622A1 - 吸収冷凍機 - Google Patents
吸収冷凍機 Download PDFInfo
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- WO2004046622A1 WO2004046622A1 PCT/JP2003/012250 JP0312250W WO2004046622A1 WO 2004046622 A1 WO2004046622 A1 WO 2004046622A1 JP 0312250 W JP0312250 W JP 0312250W WO 2004046622 A1 WO2004046622 A1 WO 2004046622A1
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- Prior art keywords
- regenerator
- absorber
- auxiliary
- solution
- refrigerant vapor
- Prior art date
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Classifications
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
- F25B15/00—Sorption machines, plants or systems, operating continuously, e.g. absorption type
- F25B15/008—Sorption machines, plants or systems, operating continuously, e.g. absorption type with multi-stage operation
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
- F25B27/00—Machines, plants or systems, using particular sources of energy
- F25B27/02—Machines, plants or systems, using particular sources of energy using waste heat, e.g. from internal-combustion engines
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A30/00—Adapting or protecting infrastructure or their operation
- Y02A30/27—Relating to heating, ventilation or air conditioning [HVAC] technologies
- Y02A30/274—Relating to heating, ventilation or air conditioning [HVAC] technologies using waste energy, e.g. from internal combustion engine
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02B—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO BUILDINGS, e.g. HOUSING, HOUSE APPLIANCES OR RELATED END-USER APPLICATIONS
- Y02B30/00—Energy efficient heating, ventilation or air conditioning [HVAC]
- Y02B30/62—Absorption based systems
- Y02B30/625—Absorption based systems combined with heat or power generation [CHP], e.g. trigeneration
Definitions
- the present invention relates to an absorption chiller, particularly hot water having a relatively low temperature, such as cooling and exhaust heat of an engine (jacket hot water), cooling and exhaust heat of a factory process, and hot water recovery heat from boiler exhaust gas.
- the present invention relates to an absorption refrigerator using hot water of about 70 ° C as a heat source.
- Exhaust heat at a relatively low temperature of about 60 to 70 ° C exists in the world in large quantities, such as engine cooling exhaust heat (jacket hot water) and factory process cooling exhaust heat. Because of the low cost, there are few uses and they are often disposed of directly or indirectly through cooling towers.
- Fig. 14 shows a single-effect type drawn on the During diagram. 3 shows an absorption cycle.
- the refrigerant evaporates in the evaporator E, moves as indicated by the broken line between E and A in the figure, and is absorbed by the absorber A.
- the diluted solution having a reduced concentration is heated by an external heat source in the regenerator G, releases the same amount of refrigerant vapor as the refrigerant evaporated in the evaporator, is concentrated, and returns to the absorber A.
- heat exchanger X is used for heat recovery (heat exchange between concentrated solution side X2 and dilute solution side X1).
- the refrigerant vapor generated in the regenerator G moves as shown by the broken line between G and C in the figure, and is condensed in the condenser C to become a refrigerant liquid.
- This refrigerant liquid returns from the condenser C to the evaporator E.
- the evaporation temperature is 5 ° C
- the absorber outlet temperature is 35 ° C
- the condensation temperature is about 35 ° C
- the solution temperature of the regenerator will be about 69 to 74 ° C
- the hot water inlet temperature as the heating source will be About 75 ° C is required.
- hot water of 65 to 70 ° C has a low temperature as a heating source. Therefore, it is impossible to produce cold water at about 7 ° C.
- the market uses chilled water below 10 ° C for air-conditioning, using waste water from around 60 to 65 ° C as a heating source, and cooling water from a cooling tower at around 30 to 31 ° C as a cooling source.
- Figure 15 shows an example of a two-stage enrichment type absorption cycle drawn on the Düring diagram where both regenerators GL and GH have almost the same area, and both absorbers AL and AH have almost the same area. Yes, shows an example of a general area-related cycle.
- the refrigerant evaporates in the evaporator E, moves as indicated by the broken line between E and A L in the figure, and is absorbed by the absorber A L.
- the dilute solution having a reduced concentration is heated by an external heat source in the low-pressure regenerator GL, releases the same amount of refrigerant vapor as the refrigerant evaporated in the evaporator, is concentrated, and returns to the absorber AL.
- the low-temperature side heat exchanger XL is used for heat recovery (heat exchange between the concentrated solution side XL2 and the dilute solution side XL1).
- the refrigerant vapor generated in the low-pressure regenerator GL moves as indicated by the broken line between GL and AH in the figure and is absorbed by the high-pressure absorber AH.
- the dilute solution having a reduced concentration in the high-pressure absorber AH is heated by an external heat source in the high-pressure regenerator GH, and has the same amount as the refrigerant generated in the low-pressure regenerator GL, that is, the same amount as the refrigerant evaporated in the evaporator E.
- the refrigerant vapor is released, concentrated and returned to the high pressure absorber AH.
- Use the high-temperature side heat exchanger XH for heat recovery of the solution (exchange heat between the concentrated solution side XH2 and the dilute solution side XH1).
- the refrigerant vapor generated in the high-pressure regenerator GH moves as indicated by the broken line between GH_C in the figure, is condensed in the condenser C, and turns into a refrigerant liquid.
- the refrigerant liquid returns from the condenser C to the evaporator E.
- the two-stage enrichment absorption refrigerator has a large number of components and a large device, and the high-pressure regenerator GH and low-pressure regenerator G have the same characteristics as the refrigerant vapor generated in the evaporator E.
- the amount of refrigerant vapor needed to be generated twice, and the thermal efficiency was less than half that of a normal single-effect absorption refrigerator, and it was rarely used in practice.
- the refrigerant evaporates in the evaporator E, moves as indicated by the broken line between E and A in the figure, and is absorbed by the absorber A.
- the diluted dilute solution at the outlet of the absorber with reduced concentration is sent to the auxiliary absorber AX, and while being cooled by the auxiliary absorber AX, the refrigerant vapor from the auxiliary regenerator GX (moves as indicated by the broken line between GX and AX in the figure) Absorb.
- the dilute solution from the diluted auxiliary absorber AX is sent to the regenerator G, and is heated and concentrated by the regenerator with an external heat source.
- the generated refrigerant vapor moves as shown by a broken line between G and C in the figure, and is condensed in the condenser C to become a refrigerant liquid.
- the refrigerant liquid returns from the condenser C to the evaporator E.
- the solution concentrated in the regenerator G is further heated and concentrated by the external heat source in the auxiliary regenerator GX, and returns to the absorber A.
- the generated refrigerant vapor moves as indicated by the broken line between G X and A X in the figure and is absorbed by the auxiliary absorber A X.
- the solution circulation system of this cycle includes a solution pump for sending the solution from the absorber A to the auxiliary absorber AX with a higher pressure than the absorber, and a solution pump for sending the solution from the auxiliary absorber AX to the regenerator G.
- a solution pump is required, and since the entire amount from the auxiliary absorber AX is sent to the regenerator G, balance control of the solution flow rate is required, and the system becomes complicated.
- the present invention has been made in view of the above-described conventional technology, and provides an absorption refrigerator having a more efficient and compact heat exchanger using hot water of about 60 to 70 ° C. with an improved installation position of a heat exchanger. That is the task. Disclosure of the invention
- an absorption refrigerator of the present invention includes a regenerator G for generating a refrigerant vapor and concentrating a solution; and a condenser for condensing the generated refrigerant vapor.
- C a regenerator for generating a refrigerant vapor and concentrating a solution
- condenser for condensing the generated refrigerant vapor.
- C an evaporator E for evaporating the condensed refrigerant
- an absorber A for absorbing the evaporated refrigerant vapor with a solution
- heating the concentrated solution from the regenerator G to generate refrigerant vapor.
- An auxiliary regenerator GX for further concentrating the solution; an auxiliary absorber AX for absorbing the refrigerant vapor generated in the auxiliary regenerator GX while cooling the dilute solution from the absorber A; and an absorption from the auxiliary regenerator GX.
- a low-temperature heat exchanger XL for exchanging heat between the concentrated solution guided to the device A and the dilute solution sent from the auxiliary absorber AX to the regenerator G; The dilute solution sent to the regenerator G from the regenerator G And a hot-side heat exchanger X H for heating with concentrated solution is led to the raw device G X.
- a regenerator G for generating a refrigerant vapor to condense the solution; a condenser for condensing the generated refrigerant vapor; an evaporator E for evaporating the condensed refrigerant; Absorber A, which absorbs the water in the regenerator G, and a supplementary regenerator GX, which heats the concentrated solution from the regenerator G to generate refrigerant vapor and further concentrates the solution; while cooling the dilute solution from the absorber A, An auxiliary absorber AX for absorbing the refrigerant vapor generated in the auxiliary regenerator GX; a heat transfer area of the auxiliary regenerator GX is 13 or less of a heat transfer area of the regenerator G; The heat transfer area of AX may be set to 23 or less of the heat transfer area of the absorber A.
- a regenerator G for generating a refrigerant vapor and concentrating the solution; a condenser for condensing the generated refrigerant vapor; and an evaporator E for evaporating the condensed refrigerant.
- An absorber A for absorbing the evaporated refrigerant vapor with a solution; an auxiliary regenerator G for heating the concentrated solution from the regenerator G to generate a refrigerant vapor and further concentrating;
- An auxiliary absorber AX for absorbing the refrigerant vapor generated in the auxiliary regenerator GX while cooling the dilute solution; and the solution is supplied from the absorber A to the auxiliary absorber AX, the regenerator G, the auxiliary regeneration.
- a regenerator G for generating a refrigerant vapor and concentrating the solution; a condenser for condensing the generated refrigerant vapor; and an evaporator E for evaporating the condensed refrigerant.
- An absorber A for absorbing the evaporated refrigerant vapor with a solution; an auxiliary regenerator GX for heating the concentrated solution from the regenerator to generate a refrigerant vapor and further concentrating; An auxiliary absorber AX for absorbing refrigerant vapor generated in the auxiliary regenerator GX, wherein the diluted solution is a part of a mixed dilute solution of the dilute solution of the outlet of the absorber A and the dilute solution of the auxiliary absorber AX as the dilute solution.
- An auxiliary absorber AX configured to use the mixed dilute solution; and a path 2 for sending the remainder of the mixed dilute solution to the regenerator G; Low temperature side heated by concentrated solution led to absorber A A high-temperature heat exchanger for heating the mixed dilute solution exiting the low-temperature heat exchanger XL and sent to the regenerator G with a concentrated solution guided from the regenerator G to the auxiliary regenerator GX; It can also be used as an absorption refrigerator equipped with XH.
- the absorber A is divided into a low-pressure evaporator AL and a high-pressure evaporator AH
- the evaporator E is divided into a low-pressure evaporator EL and a high-pressure evaporator EH.
- 10 may first be led to the high-pressure evaporator EH, and the cooled cold water 10 may then be led to the low-pressure evaporator EL.
- the concentrated solution from the auxiliary regenerator GX is first led to the low-pressure absorber AL, and the refrigerant vapor from the low-pressure evaporator E is absorbed.
- the solution that has absorbed the refrigerant vapor may be guided to the high-pressure absorber AH, the refrigerant vapor from the high-pressure evaporator EH may be absorbed, and the dilute solution that has absorbed the refrigerant vapor may be guided to the auxiliary absorber AX.
- the concentrated solution from the regenerator G is first guided to the low-pressure absorber AL, and the refrigerant vapor from the low-pressure evaporator EL is absorbed.
- the solution having absorbed the vapor is led to the high-pressure absorber AH, and the refrigerant vapor from the high-pressure evaporator EH is absorbed.
- a part of the dilute solution mixed with the solution AX may be configured to send the remainder to the regenerator G.
- This application was filed in Japanese Patent Application No. 200-2002 filed on September 26, 2002 in Japan. 801 11, based on Japanese Patent Application No. 2002-280 1112 filed on Sep. 26, 2002 and Japanese Patent Application No. 2003-166 181 filed on Jun. 11, 2003.
- the content forms a part of the content of the present application.
- FIG. 1 is a flow configuration diagram showing an absorption refrigerator according to a first embodiment of the present invention.
- FIG. 2 is a During diagram of the solution cycle of FIG.
- FIG. 3 is a graph showing the relationship between the amount of refrigerant vapor transfer between GX and AX in FIG. 1, the required hot water inlet temperature, and the COP.
- FIG. 4 is a graph showing the relationship between the refrigerant vapor transfer amount between GX and AX in FIG. 1 and the cooling water inlet temperature of the hot water inlet temperature.
- FIG. 5 is a flow configuration diagram showing an absorption refrigerator according to the second embodiment of the present invention.
- FIG. 6 is a During diagram of the solution cycle of FIG.
- FIG. 7 is a flowchart illustrating an absorption refrigerator according to the third embodiment of the present invention.
- FIGS. 8A and 8B are During diagrams in which the solution cycle of FIG. 7 is partially modified.
- FIG. 9 is a schematic configuration diagram illustrating an absorption refrigerator of a fourth embodiment of the present invention.
- FIG. 10 is a schematic configuration diagram illustrating an absorption refrigerator of a fifth embodiment of the present invention.
- FIG. 11 is a During diagram of the solution cycle for FIG.
- FIG. 12 is a schematic configuration diagram showing an absorption refrigerator of a sixth embodiment of the present invention.
- FIG. 13 is a During diagram of the solution cycle for FIG. Fig. 14 is a During diagram of a single-effect absorption cycle.
- Fig. 15 is a During diagram of a two-stage enrichment absorption cycle.
- FIG. 16 is a During diagram of a cycle that connects two separate cycles of a known two-stage enrichment absorption cycle. BEST MODE FOR CARRYING OUT THE INVENTION
- FIG. 1 is a flow configuration diagram showing an absorption refrigerator according to a first embodiment of the present invention.
- E is the evaporator
- A is the absorber
- G is the regenerator
- C is the condenser
- AX is the auxiliary absorber
- GX is the auxiliary regenerator
- XL is the low-temperature heat exchanger
- XH is the high-temperature heat Exchanger
- SP is a solution pump
- RP is a refrigerant pump
- VI is a three-way valve
- 1-4 is a solution flow path
- 5 is a refrigerant vapor flow path
- 6 is a refrigerant flow path
- 8 is hot water
- 9 is cooling water
- 10 is cold water.
- the evaporator E is formed in the same space as the absorber A via the eliminator.
- the regenerator G is formed in another identical space via the condenser C and the eliminator.
- the auxiliary absorber A X, auxiliary regenerator G X, low-temperature heat exchanger X L, and high-temperature heat exchanger X H are each formed in an independent can body.
- a refrigerant pump RP is inserted and arranged in the refrigerant flow path 7 for circulating the refrigerant.
- the auxiliary absorber AX and the regenerator G are connected by the solution flow path 2 that sends the dilute solution from the auxiliary absorber AX to the regenerator G, and in between, the low-temperature heat exchanger XL and the high-temperature heat exchanger XH Are arranged in this order, and a solution pump SP is inserted between the auxiliary absorber AX and the low-temperature side heat exchanger XL.
- the absorber A and the auxiliary absorber AX are connected by a solution flow path 1 for sending a dilute solution from the absorber A to the auxiliary absorber AX.
- regenerator G and the auxiliary regenerator GX are connected by a solution flow path 3 that sends a concentrated solution from the regenerator G to the auxiliary regenerator GX, and the high-temperature side heat exchanger XH is inserted and arranged in the solution flow path 3. .
- the auxiliary regenerator GX and the absorber A The liquid flow path 4 is connected, and a low-temperature side heat exchanger XL is inserted and arranged in the solution flow path 4. Further, the auxiliary regenerator GX and the auxiliary absorber AX are connected by a refrigerant vapor flow path 5 that sends refrigerant vapor from the auxiliary regenerator GX to the auxiliary absorber AX.
- the condenser C and the evaporator E are provided with a refrigerant passage 6 for sending the refrigerant liquid from the condenser to the evaporator E.
- a hot water pipe 81 for flowing hot water 8 as a heat source fluid for heating the solution is laid from the regenerator G to the auxiliary regenerator GX.
- the hot water 8 first flows into the regenerator G through the hot water pipe 81, and further flows into the auxiliary regenerator GX through the hot water pipe 81.
- a three-way valve V1 for adjusting the amount of hot water passing through the auxiliary regenerator GX is provided on the outlet side of the auxiliary regenerator GX of the hot water pipe 81.
- the three-way valve VI may be provided on the inlet side of the auxiliary regenerator G X in the hot water piping 81.
- a cooling water pipe 91 for flowing a cooling water 9 as a cooling medium for cooling the solution is laid from the absorber A to the condenser and to the auxiliary absorber XA.
- the cooling water 9 flows first through the cooling water pipe 91 into the absorber A, further through the cooling water pipe 91 into the condenser and then into the auxiliary absorber AX.
- the concentrated solution guided to the absorber A absorbs the refrigerant vapor from the evaporator E while being cooled by the cooling water 9, and becomes a dilute solution.
- the dilute solution from the absorber A is guided from the flow path 1 to the auxiliary absorber AX, where it absorbs the refrigerant vapor from the flow path 5 generated by the auxiliary regenerator GX while being cooled by the cooling water, and has a lower concentration. It becomes a dilute solution.
- the dilute solution exiting the auxiliary absorber AX is pressurized by the solution pump SP from the flow path 2 and enters the low-temperature heat exchanger XL, and passes from the auxiliary regenerator GX through the flow path 4 at the low-temperature heat exchanger XL. It exchanges heat with the concentrated solution going to absorber A, and the temperature of the diluted solution rises, while the temperature of the concentrated solution falls. The dilute solution then exchanges heat with the concentrated solution flowing from the regenerator G to the auxiliary regenerator GX in the high-temperature heat exchanger XH, and the temperature of the dilute solution further increases, while the temperature of the concentrated solution decreases.
- the solution is heated by hot water 8 as a heat source, generates refrigerant vapor, and is concentrated.
- the concentrated concentrated solution enters the auxiliary regenerator GX from the channel 3 via the heating side of the high-temperature side heat exchanger XH, is heated by the hot water 8 as a heat source, generates refrigerant vapor, and is further concentrated.
- Flow channel 4 leads to absorber A via the heating side of low-temperature side heat exchanger XL, One cycle of the solution cycle.
- the refrigerant liquid cools the chilled water 10 with latent heat of vaporization, becomes refrigerant vapor, and is absorbed by the solution in the absorber A.
- the refrigerant vapor generated in the regenerator G is cooled by the cooling water 9 in the condenser C, becomes a refrigerant liquid, and is guided from the flow path 6 to the evaporator E.
- the conventional two-stage enrichment cycle is divided into two systems (Fig. 15), whereas it is a cycle that circulates in one system, and the concentrated solution heated by the auxiliary regenerator GX
- the heat energy of the concentrated solution is recovered from the auxiliary absorber AX to the dilute solution toward the regenerator G, and the heat energy of the concentrated solution heated by the regenerator G is further recovered to the dilute solution.
- the cycle concentration is changed by using the auxiliary regenerator GX and the auxiliary absorber AX in order to lower the required hot water temperature.
- the heat transfer area of the auxiliary regenerator G X and auxiliary absorber A X may be set according to the corresponding hot water temperature. In this figure, the heat transfer area of the auxiliary regenerator GX is about 5% of the heat transfer area of the regenerator G, and the heat transfer area of the auxiliary absorber AX is about 20% of the heat transfer area of the absorber A. This is an example.
- the heat transfer area of the auxiliary regenerator GX is reduced because the heat source temperature and the solution temperature are greatly different. Also, from this temperature relationship, the hot water that is the heat source is placed on the high-temperature side as the inlet of the regenerator G and the low-temperature side at the outlet of the regenerator G as the auxiliary regenerator GX. It is preferred to lead to the vessel GX.
- the refrigerant evaporates in the evaporator E, moves as indicated by the broken line between E_A in FIG. 2, and is absorbed by the absorber A.
- the solution leaving the absorber A enters the auxiliary absorber AX at the same temperature and concentration, absorbs the refrigerant vapor generated in the auxiliary regenerator GX, and moves from GX to AX in Fig. 2, and To a dilute solution with low concentration.
- This dilute solution passes through the heated side XL1 of the low-temperature side heat exchanger XL, and is heated by the concentrated solution guided from the auxiliary regenerator GX to the absorber A via the heating side XL2 of the low-temperature side heat exchanger.
- This dilute solution further passes through the heated side XH1 of the high-temperature side heat exchanger XH, and is heated by the concentrated solution guided from the regenerator G to the auxiliary regenerator GX via the heating side XH2 of the high-temperature side heat exchanger. Then, enter the regenerator G.
- the refrigerant vapor of the amount absorbed by the absorber A is released and becomes a concentrated solution, enters the auxiliary regenerator GX via the heating side XH2 of the high-temperature heat exchanger XH, and is heated by an external heat source Then, an amount corresponding to the amount of refrigerant absorbed by the auxiliary absorber AX is released, and the refrigerant is further concentrated and enters the absorber A via the heating side XL2 of the low-temperature side heat exchanger XL.
- the retained heat of the concentrated solution flowing from the auxiliary regenerator GX to the absorber A is transferred from the auxiliary absorber AX to the regenerator G instead of the dilute solution flowing from the absorber A to the auxiliary absorber AX.
- the concentrated heat from the regenerator G to the auxiliary regenerator GX is recovered.
- This heat recovery can increase the temperature of the solution entering regenerator G, reduce the amount of heat required to heat the solution in regenerator G, and further reduce the hot side heat exchanger heating side XH 2
- the temperature of the solution entering the auxiliary regenerator GX via the auxiliary regenerator GX can also be higher than when the dilute solution from the auxiliary absorber AX to the regenerator G is not heated at the low-temperature heat exchanger heated side XL2.
- FIGS. 3 and 4 are graphs showing the relationship between the amount of refrigerant vapor transferred between the auxiliary regenerator G X and the auxiliary absorber A X and the hot water inlet temperature.
- the amount of refrigerant vapor generated by the auxiliary regenerator GX and absorbed by the auxiliary absorber AX is lower than that of the single-effect absorption refrigerator, and if this vapor amount is reduced to zero, it becomes equivalent to single-effect. If the amount is the same as the amount of evaporation in the evaporator E, the efficiency becomes equivalent to the two-stage concentration type.
- the amount of refrigerant vapor generated in the auxiliary regenerator G X and absorbed by the auxiliary absorber AX changes the vital concentration and the required heating source temperature.
- Figure 3 illustrates this relationship.
- the heat transfer area of the auxiliary regenerator GX is about 15% of the heat transfer area of the regenerator G, and the heat transfer area of the auxiliary absorber AX is about 50% of the heat transfer area of the absorber A.
- the heat transfer capacity of the regenerator G is limited, and the amount of refrigerant vapor is changed.
- the amount of refrigerant vapor transferred by the auxiliary regenerator GX—auxiliary absorber AX may be about half of the amount evaporated by the evaporator.
- both the auxiliary regenerator GX and the auxiliary absorber AX can be less than half the size of the regenerator G and the absorber A, respectively, which is more compact than the two-stage concentration type absorption refrigerator. And efficiency can be improved.
- the heat transfer area of the auxiliary regenerator GX is 1/3 of the heat transfer area of the regenerator G, especially about 20%, and the heat transfer area of the auxiliary absorber AX is 23, especially about the heat transfer area of the absorber A. Up to about 60%, the concentration at the outlet of the absorber is lower than the concentration at the outlet of the regenerator, and the efficiency is often better than that of a complete two-stage concentration absorption refrigerator with separate cycles.
- Figure 4 shows the required hot water temperature when the cooling water temperature changes. Therefore, even if the heat source temperature that can be supplied is the same, if the cooling water temperature decreases, the amount of refrigerant vapor generated in the auxiliary regenerator GX and absorbed by the auxiliary absorber AX can be reduced, and efficiency can be improved. Can be.
- the amount of refrigerant vapor generated by the auxiliary regenerator GX and absorbed by the auxiliary absorber AX can be calculated, for example, by providing a three-way valve V1 as shown in Fig. 1 for adjusting the amount of hot water introduced into the auxiliary regenerator GX. It is adjustable.
- the amount of generated steam is changed by partially or completely bypassing the solution flow rate to the auxiliary regenerator GX, or the solution flow rate to the auxiliary absorber AX is partially or completely bypassed for absorption. It is also possible to change the amount of steam.
- the cooling water flow rate to the auxiliary absorber AX may be changed.
- the efficiency from the two-stage enrichment absorption cycle to the single-effect absorption cycle is continuously changed by adjusting the amount of refrigerant vapor generated by the auxiliary regenerator GX and absorbed by the auxiliary absorber AX. It can be used effectively when the temperature of hot water rises or the temperature of cooling water falls, and the efficiency can be increased.
- FIG. 5 is a front view showing the structure of an absorption refrigerator according to a second embodiment of the present invention.
- Evaporator E is divided into low-pressure evaporator EL and high-pressure evaporator EH.
- the low-pressure absorber A L and the low-pressure evaporator EL are formed in the same space via an eliminator, and the high-pressure absorber AH and the high-pressure evaporator E H are formed in another same space via an eliminator.
- the cooling water pipe 91 is laid so as to flow in parallel to the low-pressure absorber AL and the high-pressure AH, and the cooling water pipe 10a runs from the high-pressure evaporator EH to the low-pressure evaporator EL in this order. It is laid in series so that it flows into.
- the solution flow path 4 is laid from the auxiliary regenerator XL through the low-temperature heat exchanger XL to the low-pressure absorber AL. Next, it is laid so that the solution is guided from the low pressure absorber A L to the high pressure absorber AH.
- the cold water 10 is first guided to the high-pressure evaporator EH, the cooled cold water 10 is then guided to the low-pressure evaporator EL, and the concentrated solution from the auxiliary regenerator GX is first guided to the low-pressure absorber AL.
- the refrigerant vapor from the low-pressure evaporator EL is absorbed, the solution in which the refrigerant vapor is absorbed by the low-pressure absorber AL is led to the high-pressure absorber AH, and the refrigerant vapor from the high-pressure evaporator EH is absorbed.
- the solution that has absorbed the refrigerant vapor in the high-pressure absorber AH passes from the flow path 1 through the auxiliary absorber AX, and from the flow path 2 passes through the low-temperature heat exchanger XL and the high-temperature heat exchanger XH to the regenerator G.
- the solution concentrated in the regenerator G is sent to the auxiliary regenerator GX from the channel 3 via the high-temperature heat exchanger XH, and is absorbed at low pressure from the channel 4 via the low-temperature heat exchanger XL.
- the vessel is led to AL.
- FIG. 6 shows the solution cycle for FIG. 5 on a Düring diagram, in which the saturation temperature of the high-pressure evaporator E H increases and the concentration of the dilute solution leaving the high-pressure absorber A H decreases.
- the amount of refrigerant required to further reduce the concentration in the auxiliary absorber AX can be reduced, and the efficiency can be increased as compared with the case of FIG.
- FIG. 7 is a flowchart illustrating an absorption refrigerator according to the third embodiment of the present invention. 7 differs from the first embodiment described with reference to FIG. 1 in that flow control valves V GH, VGS, VAW, and VAS are provided. These are three-way valves in the present embodiment.
- the flow control valve VGH is disposed in the hot water pipe 81 similarly to the three-way valve VI described in the first embodiment.
- the flow control valve VGS is located in the solution flow path 3 that connects the high-temperature side heat exchanger XH and the auxiliary regenerator GX, and the port of the three-way valve VGS connects the auxiliary regenerator GX and the low-temperature side heat exchanger XL. It is connected to the solution flow path 4 to be connected.
- the flow control valve VAW is provided on the outlet side of the auxiliary absorber AX in the cooling water pipe 91. ing.
- the three-way valve V AW may be provided on the cooling water pipe 91 on the inlet side of the auxiliary absorber AX.
- the flow control valve VAS is located in the solution flow path 1 that connects the absorber A and the auxiliary absorber AX, and the port 1 of the three-way valve VAS connects the auxiliary absorber AX and the low-temperature side heat exchanger XL. Connected between the auxiliary absorber AX of the solution flow path 2 and the solution pump SP.
- the duling cycle of the present embodiment is the same as that described with reference to FIG. FIG. 8 shows a During cycle according to a modification of the third embodiment. As shown in Fig. 8 (a), the efficiency is slightly sacrificed, but the low-temperature side heat exchanger XL can be omitted and the size can be reduced. Further, as shown in FIG. 8 (b), the heated side XL1 of the low-temperature side heat exchanger XL can be a dilute solution flowing from the absorber to the auxiliary absorber.
- the refrigerant vapor amount generated in the auxiliary regenerator GX and absorbed by the auxiliary absorber AX is obtained by introducing a three-way valve VGH to the auxiliary regenerator GX as shown in FIG. 7, for example. If it is provided to adjust the amount of hot water, it can be adjusted. Also, by using the solution valve VGS shown in Fig. 7 to partially or fully bypass the solution flow rate to the auxiliary regenerator GX as shown by the broken line, the amount of generated steam is limited, and the gas is moved between GX and AX. Refrigerant vapor amount can be changed. Also, change the cooling water flow rate to the auxiliary absorber AX with the cooling water valve VAW in Fig.
- the amount of refrigerant vapor moving between GX and AX can be changed by limiting the amount of absorbed vapor.
- the efficiency from the two-stage concentrated absorption cycle to the single-effect absorption cycle is continuously changed by adjusting the amount of refrigerant vapor generated by the auxiliary regenerator GX and absorbed by the auxiliary absorber AX. It can be used effectively when the temperature of hot water rises or the temperature of cooling water falls, and efficiency can be increased.
- FIG. 9 is a schematic configuration diagram illustrating an absorption refrigerator of a fourth embodiment of the present invention.
- the refrigerator of the present embodiment includes an evaporator E, an absorber A, a regenerator G, It consists of condenser C, auxiliary absorber AX, auxiliary regenerator GX, low-temperature heat exchanger XL, and high-temperature heat exchanger XH.
- the difference of the present embodiment from the first embodiment is that the solution flow path 1a from the absorber A merges with the solution flow path 2a from the auxiliary absorber AX and is sucked into the solution pump SP. And the point that the solution flow path 1b to the auxiliary absorber AX branches off from the solution flow path 2 from the outlet of the solution pump SP.
- the concentrated solution guided to the absorber A absorbs the refrigerant vapor from the evaporator E while being cooled by the cooling water 9, and becomes a dilute solution.
- the dilute solution from the absorber A is pressurized by the solution pump SP and mixed with the dilute solution from the auxiliary absorber AX.
- a part of the mixed dilute solution is guided to the auxiliary absorber AX, and absorbs the refrigerant vapor generated in the auxiliary regenerator GX while being cooled by the cooling water 9, and becomes a dilute solution having a lower concentration.
- the remaining mixed dilute solution pressurized by the solution pump SP enters the low-temperature side heat exchanger XL, and exchanges heat with the concentrated solution flowing from the auxiliary regenerator GX to the absorber A in the low-temperature side heat exchanger XL and mixes.
- Dilute solutions increase in temperature, while concentrated solutions decrease in temperature.
- the mixed dilute solution then enters the high-temperature heat exchanger XH, and exchanges heat with the concentrated solution from the regenerator G to the auxiliary regenerator GX in the high-temperature heat exchanger XH, and the mixed dilute solution further rises in temperature.
- the temperature of a concentrated solution decreases.
- the solution is heated by hot water as a heat source, generates refrigerant vapor, and is concentrated.
- the concentrated concentrated solution passes through the heating side of the high-temperature side heat exchanger XH and enters the auxiliary regenerator GX, where it is heated by the hot water of the heat source to generate refrigerant vapor, which is further concentrated and exchanged on the low-temperature side.
- the liquid is led to absorber A via the heating side of vessel XL, and goes through a solution cycle.
- the refrigerant liquid cools the chilled water by the latent heat of evaporation and becomes refrigerant vapor, which is absorbed by the solution in the absorber A.
- the refrigerant vapor generated in the regenerator G is cooled by the cooling water 9 in the condenser C, and is introduced into the evaporator E as a refrigerant liquid.
- the conventional two-stage enrichment cycle is a cycle that circulates in one system, while the cycle is divided into two systems (Fig. 15), and the enrichment heated by the auxiliary regenerator GX.
- the thermal energy of the solution is recovered from the auxiliary absorber AX to the dilute solution going to the regenerator G, and the thermal energy of the concentrated solution heated by the regenerator G is further recovered to the dilute solution.
- the solution circulation system requires a solution pump at the outlet of the absorber and a solution pump at the outlet of the auxiliary absorber, and enters and exits the auxiliary absorber. A balance control of the solution flow was required.
- the solution from the auxiliary absorber AX is not sent to the regenerator G, but is sent from the auxiliary absorber AX to the outlet side of the lower-pressure absorber A.
- the solution pump at the AX outlet becomes unnecessary.
- FIG. 11 shows the cycle on the During diagram, and the solution cycle for FIG. 9 is shown on the During diagram.
- the amount of refrigerant vapor generated by the auxiliary regenerator GX and absorbed by the auxiliary absorber AX is lower than that of the single-effect absorption refrigerator.
- this steam amount is set to zero, it is equivalent to single-effect, and if it is equal to the amount of evaporation in the evaporator E, the efficiency is equivalent to the two-stage concentration type.
- the efficiency of the refrigerator increases.
- the concentration of the solution at the outlet of the auxiliary absorber increases, and the condensation temperature does not decrease, so that the heating source temperature required for the regenerator increases.
- the solution concentration at the outlet of the auxiliary absorber decreases, and the condensation temperature also decreases, so that the heating source temperature required for the regenerator can be reduced.
- the amount of refrigerant vapor generated by the auxiliary regenerator GX and absorbed by the auxiliary absorber AX may be controlled.
- a fifth embodiment which is an improvement of FIG. 9, is shown in the schematic configuration diagram of FIG.
- the absorption refrigerator of the present embodiment includes a method of adjusting the amount of refrigerant vapor generated in auxiliary regenerator GX and absorbed in auxiliary absorber AX.
- the valve VA is arranged in the hot water pipe 81 similarly to the three-way valve V1 described in the first embodiment.
- the three-way valve VD is arranged in a solution flow path 1b from the solution pump SP to the auxiliary absorber AX, and a port of the three-way valve VD is connected to the auxiliary absorber AX.
- the port 1 of the three-way valve VD may be connected to the suction side of the solution pump SP, that is, the solution flow path 2a or the solution flow path 1a, instead of the auxiliary absorber AX.
- the three-way valve V C is provided on the cooling water pipe at the outlet side of the auxiliary absorber AX.
- the three-way valve VC may be provided on the inlet side of the auxiliary absorber AX of the cooling water pipe.
- the three-way valve VB is located in the solution flow path 3 that connects the high-temperature side heat exchanger XH and the auxiliary regenerator GX, and one port of the three-way valve VB connects the auxiliary regenerator GX and the low-temperature side heat exchanger XL. Connected to the solution flow path 4.
- the heat source heat amount required for the auxiliary regenerator GX is small and the required temperature is also reduced.
- the heat source temperature required for regenerator G remains high. It is desirable that the heat source fluid is first guided to the regenerator G and then to the auxiliary regenerator GX. That is, since a high heat source temperature can be used on the regenerator G side, the efficiency is easily increased.
- the control of the amount of refrigerant vapor generated by the auxiliary regenerator GX and absorbed by the auxiliary absorber AX be adjusted by the adjusting end so that the heat source temperature (heat source outlet temperature) becomes a target value.
- the heat source inlet temperature also decreases.
- the detection position of the heat source may not be specified. Generally, it is the heat source outlet temperature or the heat source inlet temperature.
- FIG. 12 is a schematic configuration diagram showing an absorption refrigerator of a sixth embodiment of the present invention. This embodiment can be said to be a modification of the fourth embodiment.
- the absorber A of the absorption refrigerator is replaced with a low-pressure absorber A.
- Evaporator E is divided into high-pressure absorber AH, evaporator E is divided into low-pressure evaporator EL and high-pressure evaporator EH.Cold water is first introduced into high-pressure evaporator EH, cooled cold water is introduced into low-pressure evaporator EL, and auxiliary regeneration is performed.
- the concentrated solution from the device GX is first led to the low-pressure absorber AL, the refrigerant vapor from the low-pressure evaporator EL is absorbed, and the solution in which the refrigerant vapor is absorbed by the low-pressure absorber AL is guided to the high-pressure absorber AH. It absorbs refrigerant vapor from EH.
- Fig. 13 shows the solution cycle for Fig. 12 on a Douling diagram, where the saturation temperature of the high-pressure evaporator EH increases and the concentration of the dilute solution leaving the high-pressure absorber AH decreases.
- the amount of concentration required to be further reduced by the auxiliary absorber AX can be reduced, and the efficiency can be increased as compared with the case of FIG.
- the cooling water flow be branched at the cooling water introduction port, with one flowing through the condenser-absorption refrigerator and the other flowing into the auxiliary absorber, since the required hot water temperature may be low.
- an absorption refrigerator including a regenerator, a condenser, an absorber, an evaporator, an auxiliary regenerator and an auxiliary absorber
- the concentrated solution is further concentrated by heating the concentrated solution with the auxiliary regenerator to generate refrigerant vapor and absorbing the refrigerant vapor from the auxiliary regenerator while cooling the dilute solution from the absorber with the auxiliary absorber.
- a low-temperature side heat exchanger that exchanges heat between the concentrated solution guided from the auxiliary regenerator to the absorber and the dilute solution sent from the auxiliary absorber to the regenerator, Further, there is provided a high-temperature side heat exchanger for heating the dilute solution exiting the low-temperature side heat exchanger and sent to the regenerator with a concentrated solution guided from the regenerator to the auxiliary regenerator.
- the absorber is divided into a low-pressure absorber and a high-pressure absorber, and the evaporator is divided into a low-pressure evaporator and a high-pressure evaporator.
- the concentrated solution from the auxiliary regenerator is first guided to a low-pressure absorber, where the refrigerant vapor from the low-pressure evaporator is absorbed, and the solution in which the refrigerant vapor is absorbed by the low-pressure absorber is absorbed at a high pressure.
- the dilute solution can be guided to the auxiliary absorber by absorbing the refrigerant vapor from the high-pressure evaporator.
- an absorption refrigerator of another embodiment of the present invention in an absorption refrigerator including a regenerator, a condenser, an absorber, an evaporator, an auxiliary regenerator and an auxiliary absorber, the concentration from the regenerator is provided.
- the solution is heated by the auxiliary regenerator to generate a refrigerant vapor and further concentrated, While the dilute solution from the absorber is cooled by the auxiliary absorber, the refrigerant vapor from the auxiliary regenerator is absorbed, and the heat transfer area of the auxiliary regenerator is set to the heat transfer area of the regenerator. 1 Z 3 or less, and the heat transfer area of the auxiliary absorber may be 23 or less of the heat transfer area of the absorber.
- the heat source fluid can be guided first to the regenerator and then to the auxiliary regenerator.
- An absorption refrigerator includes a regenerator, a condenser, an absorber, an evaporator, an auxiliary regenerator, and an auxiliary absorber, and the absorbing solution is supplied from the absorber to the auxiliary absorber to the regenerator.
- means for adjusting the heat transfer capacity of the auxiliary regenerator and / or means for adjusting the heat transfer capacity of the auxiliary absorber may be provided.
- the absorber is divided into a low-pressure absorber and a high-pressure absorber
- the evaporator is divided into a low-pressure evaporator and a high-pressure evaporator.
- the cold water was then led to the low-pressure evaporator, and the concentrated solution from the regenerator and auxiliary regenerator was first led to the low-pressure absorber, where the refrigerant vapor from the low-pressure evaporator was absorbed, and the refrigerant vapor was absorbed by the low-pressure absorber.
- the solution may be guided to a high-pressure absorber to absorb the refrigerant vapor from the high-pressure evaporator, and the dilute solution may be guided to the auxiliary regenerator.
- the means for adjusting the heat transfer capability of the auxiliary regenerator may include: bypassing the auxiliary regenerator and adjusting the flow rate of hot water flowing through the auxiliary regenerator or a hot water flow control valve; or It can be a solution flow rate control valve for controlling the flow rate of the passing solution.
- the means for adjusting the heat transfer capacity of the auxiliary absorber is a cooling water flow rate control valve that adjusts a flow rate of cooling water that bypasses and / or passes through the auxiliary absorber, or a heat transfer unit of the auxiliary absorber.
- an absorption refrigerator including a regenerator, a condenser, an absorber, an evaporator, an auxiliary regenerator and an auxiliary absorber, wherein the concentrated solution from the regenerator Is heated by the auxiliary regenerator to generate a refrigerant vapor and further concentrated.
- the generated refrigerant vapor is mixed and diluted by the auxiliary absorber with the dilute solution at the absorber outlet and the dilute solution at the auxiliary absorber outlet.
- a path for sending the remaining part of the mixed dilute solution to the regenerator is provided.
- a low-temperature side heat exchanger heated by a concentrated solution guided from the vessel to the absorber, and a mixed dilute solution exiting the low-temperature side heat exchanger and sent to the regenerator are guided from the regenerator to the auxiliary regenerator.
- a hot side heat exchanger for heating with a concentrated solution is provided.
- the absorber of the absorption refrigerator is replaced by a low-pressure absorber and a high-pressure absorber
- the evaporator is replaced by a low-pressure evaporator and a high-pressure evaporator.
- the cold water is first guided to the high-pressure evaporator, the cooled cold water is then guided to the low-pressure evaporator, and the concentrated solution from the regenerator is first guided to the low-pressure absorber, and the refrigerant vapor from the low-pressure evaporator
- the dilute solution that absorbed the refrigerant vapor from the high-pressure evaporator, absorbed the refrigerant vapor from the high-pressure evaporator, and absorbed the refrigerant vapor from the high-pressure absorber into the auxiliary absorber. It may be mixed with the dilute solution from the above to make a mixed dilute solution, a part of which is led to the auxiliary absorber, and the remaining part is led to the regenerator.
- an absorption refrigerator using hot water of about 60 to 70 ° C. as a heat source is inferior to a single-effect absorption refrigerator, but is a two-stage concentration type.
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- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Combustion & Propulsion (AREA)
- Sorption Type Refrigeration Machines (AREA)
Description
Claims
Priority Applications (5)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US10/529,438 US7398656B2 (en) | 2002-09-26 | 2003-09-25 | Absorption refrigerating machine |
AU2003266614A AU2003266614A1 (en) | 2002-09-26 | 2003-09-25 | Absorption refrigerating machine |
EP03811491A EP1548378A4 (en) | 2002-09-26 | 2003-09-25 | ABSORPTION REFRIGERATION MACHINE |
JP2004553137A JP4376788B2 (ja) | 2002-09-26 | 2003-09-25 | 吸収冷凍機 |
US12/155,883 US7827821B2 (en) | 2002-09-26 | 2008-06-11 | Absorption refrigerating machine |
Applications Claiming Priority (6)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP2002280112 | 2002-09-26 | ||
JP2002-280111 | 2002-09-26 | ||
JP2002280111 | 2002-09-26 | ||
JP2002-280112 | 2002-09-26 | ||
JP2003-166181 | 2003-06-11 | ||
JP2003166181 | 2003-06-11 |
Related Child Applications (2)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
US10529438 A-371-Of-International | 2003-09-25 | ||
US12/155,883 Division US7827821B2 (en) | 2002-09-26 | 2008-06-11 | Absorption refrigerating machine |
Publications (1)
Publication Number | Publication Date |
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WO2004046622A1 true WO2004046622A1 (ja) | 2004-06-03 |
Family
ID=32329636
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/JP2003/012250 WO2004046622A1 (ja) | 2002-09-26 | 2003-09-25 | 吸収冷凍機 |
Country Status (5)
Country | Link |
---|---|
US (2) | US7398656B2 (ja) |
EP (1) | EP1548378A4 (ja) |
JP (1) | JP4376788B2 (ja) |
AU (1) | AU2003266614A1 (ja) |
WO (1) | WO2004046622A1 (ja) |
Families Citing this family (3)
Publication number | Priority date | Publication date | Assignee | Title |
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FR2900721B1 (fr) * | 2006-05-02 | 2008-08-29 | Peugeot Citroen Automobiles Sa | Dispositif de refroidissement par absorption et vehicule automobile associe. |
AT12048U1 (de) * | 2010-03-23 | 2011-09-15 | Stefan Ing Petters | Vorrichtung zur übertragung von wärme |
CN107144043A (zh) * | 2017-06-28 | 2017-09-08 | 远大空调有限公司 | 一种三段式热水机组系统及其工作方法 |
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- 2003-09-25 JP JP2004553137A patent/JP4376788B2/ja not_active Expired - Fee Related
- 2003-09-25 WO PCT/JP2003/012250 patent/WO2004046622A1/ja active Application Filing
- 2003-09-25 US US10/529,438 patent/US7398656B2/en not_active Expired - Fee Related
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Also Published As
Publication number | Publication date |
---|---|
US20060144078A1 (en) | 2006-07-06 |
US20080250811A1 (en) | 2008-10-16 |
EP1548378A4 (en) | 2012-09-19 |
US7398656B2 (en) | 2008-07-15 |
JP4376788B2 (ja) | 2009-12-02 |
US7827821B2 (en) | 2010-11-09 |
AU2003266614A1 (en) | 2004-06-15 |
EP1548378A1 (en) | 2005-06-29 |
JPWO2004046622A1 (ja) | 2006-03-16 |
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